Fluid bed filter-dryer apparatus

ABSTRACT

A filter-dryer apparatus employing a single container for both filtering and drying operations including a container holding a material to be filtered and dried, adapted to connect to a filter system and to connect to a fluid bed dryer system, and a process for separating particulates from liquids by the operations of filtration and drying, which includes the steps of providing a single container for both filtering and drying operations; introducing a mixture of particles and liquid to said container; connecting the container to a filter system and filtering the particulates from the liquid; detaching the container from the filter system; connecting the container to a fluid bed drying system and removing the liquid from the particulates to result in dry particulates.

BACKGROUND OF THE INVENTION

[0001] This invention is generally directed to an apparatus and methodsof its use for separating particulates from liquids by filtration andfurther removing liquids from the particulates by drying. The presentinvention is greatly efficient in filtering and drying to yield a highquality product by employing a single container for both filtering anddrying operations.

[0002] As known, particularly in producing chemical and pharmaceuticalcompositions, use is made of large filtration chambers and fluid-beddryers. The filtration chambers generally consist of vessels, usuallycylindrical, comprising a bottom part, a filter plate assembly, and atop part having diameters between 300 and 5,000 mm. The filtrationchambers are used to remove liquids from particulate materials andsolids.

[0003] Furthermore, the solids can be transferred to a fluid-bed dryerthat uses a gas stream to remove moisture from the solids.Significantly, during the transfer of the solids from the filtrationchamber to the fluid-bed dryer, the solids can be contaminated, spilled,lost, and/or degraded.

BRIEF SUMMARY OF THE INVENTION,

[0004] The present invention provides a method and apparatus by meanswhich a particulate material is filtered and dried in a single productcontainer.

[0005] Performing both filtering and drying operations in a singleproduct container reduces the risk of contaminating, degrading, orlosing the particulate material.

[0006] The apparatus of the present invention filters and dries aparticulate material having a liquid (e.g. solvent) content andcomprises a single product container holding the material, that fits andadapts to a pressure filter system and a fluid-bed dryer system.Examples of typical solvents include the following: water, isopropylalcohol, acetone, methyl alcohol, ethylene dichloride, methyl chloride,toluene, xylene, benzene, methyl ethyl ketone and hexane. Particleshapes of the particulate material have sphericity shape factors of 0.3to 1.0 (1.0 being a sphere). The particulate sizes range from 1 μm to20,000 μm, and more commonly from 2 μm to 10,000 μm.

[0007] Regarding “shape factors”, it is understood that many particlesin packed beds are often irregular in shape. The equivalent diameter ofa particle is defined as the diameter of a sphere having the same volumeas this particle. Sphericity shape factor of a particle is the ratio ofthe surface area of this sphere having the same volume as the particleto the actual surface area of the particle.

[0008] The product container includes a vessel, usually cylindrical,having a detachable bottom plate forming a support for a filteringassembly. The filter assembly comprises a filter sheet and a filternetting bed, both anchored to the bottom plate. The bottom plate can beremoved.

[0009] The product container also includes a detachable upper plateforming a support for a gas distribution plate. The gas distributionplate comprises a perforated, sintered, or grid plate with or without aretention screen. The gas distribution plate can be installed before orafter the filtering process.

[0010] After filtering the particulate material, the gas distributionplate is installed and the product container is inverted. The gasdistribution plate supports the filtered material in the invertedposition. The filter plate assembly is then removed from the productcontainer.

[0011] The product container is installed into a fluid-bed dryer system.The fluid-bed dryer system consists of a lower plenum, an upper plenum,a dust collector, and a gas handling system. The gas handling systemcomprises at least one of a heater, a pressure blower, and a condenser.

[0012] The product container is installed between the lower and upperplenums. The gas (for example, air, argon, nitrogen, and carbon dioxide)stream is introduced into lower plenum. The gas stream flows through thegas distribution plate and the particulate material. The solvent in theparticulate material is removed by the gas stream.

[0013] A filtering device in the upper plenum, above the productcontainer, removes particulates in the gas stream and may be recycled.The solvent can be condensed from the gas stream and retrieved. The gasstream can be recycled to the dryer or vented to the atmosphere.

[0014] After the particulate material is adequately dried, the productis removed from the product container for packaging or additionalprocessing.

BRIEF DESCRIPTION OF THE DRAWINGS

[0015]FIG. 1 is a side view with cut away of the product containeradapted to filtration device.

[0016]FIG. 2 is a side view with cut away of the product containerprepared for adapting to dryer.

[0017]FIG. 3 is a side view of a trolley used to transport the productcontainer.

[0018]FIG. 4 is a side view of the product container adapted to dryingdevice.

[0019]FIG. 5 is a side view of an embodiment of the product containerwherein the diameter of the container is smaller at the gas distributionplate.

[0020]FIG. 6 is a side view of an embodiment of the product containeradapted to a drying device wherein the fluid-bed assembly has an upperplenum having the same diameter as the container.

[0021]FIG. 7 shows gas stream flows out of the fluid-bed assemblyoperated to generate different types of fluidization.

[0022]FIG. 8 is a side view of an embodiment of the product containeradapted to a filtering-drying assembly wherein the inlet head is notremoved between the filtering and drying process and the discharge headis also used as the upper plenum.

[0023]FIG. 9 is a side view of an embodiment of the product containeradapted to a filtering-drying assembly wherein the gas stream flows intothe inlet nozzle and the outlet nozzle during the drying process.

DETAILED DESCRIPTION OF THE INVENTION

[0024] The present invention provides a method and apparatus by meanswhich a particulate material is filtered and dried in a single productcontainer.

[0025] The product container 10 is usually mounted on a trolley 15 thatallows the container to be moved to and from the processing areas (FIG.1). The trolley 15 can have a system that allows the product containerto invert. Furthermore, a lifting/rotating device can be utilized toperform the product bowl inversion.

[0026] The liquid/solids are introduced into the product container 10with the detachable filter assembly 13 attached, which are components ofthe nutsche type filter assembly shown in FIG. 1. The solvent content ofthe particulate material before filtering is 15%-90%. When the materialis fed into the product container 10, the discharge head 14 can beattached or unattached to the product container 10 shown in FIG. 1.

[0027] After the material is fed into the product container 10, theinlet head 12 to the nutsche filter assembly is attached, FIG. 1. On theinlet head 12, a gas stream is fed into the gas inlet nozzle 16 shown inFIG. 1. The gas stream pressurizes the product container 10. Theoperating pressure is 0.5 psia -100 psia at a temperature of 0-300° F.The pressure above the material forces liquid through the filteringassembly 13 shown in FIG. 1. The liquid flows through the filterassembly and into the discharge head 14 shown in FIG. 1. The liquidflows out of the discharge head through the liquid nozzle 17 shown inFIG. 1.

[0028] After some of the liquid is removed from the material, the filteris depressurized. The solvent content of the particulate material afterfiltering is 1%-50%. The inlet head 12 is removed from the productcontainer. The detachable gas distribution plate 11 is installed abovethe material in the product container 10 shown in FIG. 1.

[0029] The nutsche type filter assembly is inverted so that the gasdistribution plate 21 is on the bottom of the product container 20 shownin FIG. 2. Once the product container 20 is positioned in theorientation shown in FIG. 2, the discharge head 24 and detachable filterassembly 23 are removed from the product container 20 shown in FIG. 2.

[0030] The product container 30 with the gas distribution plate 31 istransported to the fluid-bed assembly. A trolley 35 shown in FIG. 3 canbe used to transport the product container. The trolley 35 can also beequipped with a mechanism to invert the product container. Otherwise, aseparate machine, or person(s), inverts the product container.

[0031] A detachable cover 36 shown in FIG. 3 can be used during thetransport operation. Before the product container 30, shown in FIG. 3,is installed into the fluid-bed assembly, the detachable cover 36 isremoved.

[0032] The product container 40 is installed between the upper plenum 43and lower plenum 42 of the fluid-bed assembly shown in FIG. 4. Once thelower plenum 42, product container 40, and upper plenum 43 are sealed,the gas stream is introduced into the gas inlet nozzle 44 on the lowerplenum 42. The gas flows at a velocity of 10 fpm-600 fpm at the gasdistribution plate. The gas stream flows up through the material. Theliquid evaporates in the gas stream. Particulates in the gas stream arefiltered in the upper plenum 43 by a filtering device 46 shown in FIG.4.

[0033] The gas stream flows out of the fluid-bed assembly through theexhaust nozzle 47 shown in FIG. 4. The gas flow rate is adjusted so thatthe material behaves as a fixed bed, incipient fluidization, smoothfluidization, bubbling fluidization, slugging fluidization shown in FIG.7. The gas flow rate is less than the flow rate where dilute phase ortransport fluidization occurs, which is shown in FIG. 7. The solventcontent of the particulate material after drying is 0%-20%.

[0034] An additional structural embodiment is shown in FIG. 5. In FIG.5, the product container 50 is conical such that the area of the gasdistribution plate 51 is smaller than the area of the filtering assembly53. That is, the diameter of the product container is smaller at the gasdistribution plate, which gives the product container an expansion zone.The expansion zone reduces the amount of material entrained in the gasstream during the fluidization process.

[0035] Another structural embodiment is a fluid-bed assembly with anupper plenum 63 having the same diameter as the product container 60shown in FIG. 6.

[0036] Using the inlet head 82 shown in FIG. 8 as the lower plenum isanother structural embodiment. That is, the inlet head is not removedbetween the filtering and drying process. Instead, it is used as the gaschamber directly below the gas distribution plate 81. The discharge head84 is also used as the upper plenum in this structural embodiment shownin FIG. 8. A filtering device downstream from the upper plenum removesfugitive particulates in the gas stream. The filter plate assembly 83can either be removed or left in the assembly during the drying step.The gas stream flows into the inlet nozzle 86 and out of the dischargenozzle 87.

[0037] Another structural embodiment is shown in FIG. 9. In FIG. 9, thegas stream flows into the inlet nozzle 96 and the outlet nozzle 98 onthe product container 90 during the drying process. During the filteringprocess, the gas is fed into the gas nozzle 99 on the product container90 shown in FIG. 9. The liquid removed from the material flows out ofthe outlet nozzle 97 on the discharge head 92 shown in FIG. 9.

[0038] The invention is further illustrated, but not limited, by thefollowing Examples:

EXAMPLES

[0039] The filter/dryer apparatus of the present invention was operatedand tested on several types of materials. The filter/dryer removes theliquid from a mixture of a liquid and bulk solid, where as the solid isinsoluble or soluble in the liquid.

[0040] The general procedure entailed the following:

[0041] First, 300 ml of the bulk solid was measured into a 1000 mlbeaker. Second, the liquid was added to the beaker until the materialwas completely submerged in the liquid. That is, the liquid level andbulk solid level were equal in the beaker. Third, the volume of liquidrequired to submerge the bulk solid was recorded.

[0042] Once the initial solid/liquid mixture was prepared, the mixturewas poured in a 4″ (Examples 1-4) or 16″ (Examples 5 and 6) diameterproduct container 10, which is a component of the nutsche filterassembly shown in FIG. 1. The inlet head 12 was attached to the nutschefilter assembly. On the inlet head 12, the air supply line was attachedto the gas inlet nozzle 16 and the filter was pressurized. The pressureabove the mixture forced the liquid through the filtering assembly 13,shown in FIG. 1. The liquid flowed through the filter assembly and intothe discharge head 14 shown in FIG. 1. The liquid flowed out through theliquid nozzle 17 located on the discharge head 14 shown in FIG. 1.

[0043] After 15 minutes of filtering the liquid in the nutsche filter,the filter assembly was depressurized. The amount of liquid that flowedout of the discharge head was recorded. The inlet head 12 was removedand the detachable gas distribution plate 11, shown in FIG. 1, wasinstalled. The nutsche filter assembly was inverted so that the gasdistribution plate 21 was on the bottom of the product container 20,shown in FIG. 2. Once the product container 20 was positioned in theorientation shown in FIG. 2, the discharge head 22 and detachable filterassembly 23 were removed from the product container 20 shown in FIG. 2.

[0044] The product container 30 with the gas distribution plate 31 wastransported to the fluid-bed assembly. A trolley 35 shown in FIG. 3 canbe used to transport the product container. The trolley 35 can also beequipped with a mechanism to invert the product container.

[0045] A detachable cover 36 shown in FIG. 3 can be used during thetransport operation. Before the product container 30, shown in FIG. 3,was installed into the fluid-bed assembly, the detachable cover 36 wasremoved.

[0046] In Examples 1-4, the product container 40 was installed betweenthe upper plenum 43 and lower plenum 42 of the fluid-bed assembly shownin FIG. 4. Once the lower plenum 42, product container 40, and upperplenum 43 were sealed, the gas stream was introduced into the gas inletnozzle 44 on the lower plenum 42. The gas stream flowed up through themixture of solid/liquid for 15 minutes. The liquid evaporated in the gasstream. Particulates in the gas stream were filtered in the upper plenum43 by a filtering device 46 shown in FIG. 4. The gas stream flowed outof the fluid-bed assembly through the exhaust nozzle 47 shown in FIG. 4.The rate and temperature of the gas stream was recorded. The moisturecontent of the dried material was measured by an oven moisture method.The final moisture of the dried material was recorded.

[0047] In Examples 5 and 6, the product container and gas distributionplate were transported to a fluid-bed dryer assembly shown in FIG. 6,where the upper plenum had a diameter, 16″, identical to thedistribution plate, 16″. The fluid-bed dryer assembly and productcontainer were sealed, and a heated argon gas stream, flowed up throughthe liquid at such a rate, where the bed behaved with bubblingfluidization characteristics shown in FIG. 7. After the argon gas streamfluidized the liquid/solid mixture for 120 minutes, the liquid contentof the mixture in the product bowl was measured and recorded. The gasstream in Examples 5 and 6 was recirculated. The gas stream from thefluid-bed dryer was passed through a condenser, which removed themajority of the solvent in the argon gas stream. The gas stream washeated by a heat exchanger before being recirculated to the fluid-beddryer apparatus. Since a small amount of solvent was recirculated to theinlet of the fluid-bed dryer, the recycling fluid-bed drying step tookmore time than the once through drying step described in Examples 1-4.

Example 1

[0048] A mixture of methyl alcohol, 83%, and magnesium oxide, 17%, wherethe particle range of the magnesium oxide was 5-50 μm, was fed into a 4″diameter product container, which was a component of the filter assemblyshown in FIG. 1. Compressed air was fed into the inlet head until thepressure above the mixture was 20 psig for 15 minutes. The liquid,methyl alcohol, flowed through the filter assembly and into thedischarge head. The mixture in the product container after the filteringprocess was a stiff cake of magnesium oxide and methyl alcohol with amoisture content of 31%.

[0049] The inlet head was depressurized and removed from the productcontainer. The detachable gas distribution plate was installed on theproduct container. The 4″ diameter product container was inverted so thegas distribution plate was on the bottom of the product container. Thedischarge head and detachable filter assembly were removed from theproduct container.

[0050] The product container and gas distribution plate were transportedto a fluid-bed dryer assembly shown in FIG. 4, where the upper plenumhad a larger diameter, 11″, than the product container, 4″. Thefluid-bed dryer assembly and product container were sealed, and a heatedair stream, 73° F., flowed up through the mixture of magnesiumoxide/methyl alcohol at such a rate, 120-140 ft/min at the distributionplate, whereby the bed behaved with incipient fluidizationcharacteristics shown in FIG. 7. After the air stream fluidized theliquid/solid mixture for 15 minutes, the methyl alcohol content of themixture in the product bowl was 1.4%.

[0051] The results of Example 1 show that a non-aqueous solvent, methylalcohol, can be removed from a bulk solid, magnesium oxide, with a smallparticles size distribution, 5-50 μm. The physical properties of theliquid/solid mixture was a stiff dry cake after the filtration process,a 31% moisture content. The fluid-bed dryer reduced the moisture contentof the cake from 31% to 1.4%, which was a free flowing powder, 5-50 μm.

[0052] The fluid-bed dryer apparatus used in Example 1 is shown in FIG.4, where the upper plenum has a larger diameter than the productcontainer. The larger diameter of the upper plenum 43 reduces the amountof dust on the bag filters 46 shown in FIG. 4.

Example 2

[0053] A mixture of acetone, 50%, and titanium, 50%, where the particlerange of the titanium was 250-420 μm, was fed into a 4″ diameter productcontainer, which was a component of the filter assembly shown in FIG. 1.Compressed air was fed into the inlet head until the pressure above themixture was 10 psig for 15 minutes. The liquid, acetone, flowed throughthe filter assembly and into the discharge head. The mixture in theproduct container after the filtering process had an acetone content of2%.

[0054] The inlet head was depressurized and removed from the productcontainer. The detachable gas distribution plate was installed on theproduct container. The 4″ diameter product container was inverted so thegas distribution plate was on the bottom of the product container. Thedischarge head and detachable filter assembly were removed from theproduct container.

[0055] The product container and gas distribution plate were transportedto a fluid-bed dryer assembly shown in FIG. 4, where the upper plenumhad a larger diameter, 11″, than the product container, 4″. Thefluid-bed dryer assembly and product container were sealed, and a heatedair stream, 70° F., flowed up through the mixture of titanium/acetone atsuch a rate, 280-320 ft/min at the distribution plate, whereby the bedbehaved with bubbling fluidization characteristics shown in FIG. 7.After the air stream fluidized the liquid/solid mixture for 15 minutes,the acetone content of the mixture in the product bowl was 0.01%.

[0056] Example 2 shows that the majority of liquid, 48%, can be removedduring the filtration step when the solid, titanium, does not absorb theliquid, acetone. After the filtration step, the material was a freeflowing mixture as opposed to the dry cake in Example 1.

Example 3

[0057] A mixture of water, 50%, and polyethylene (plastic) beads, 50%,where the particle range of the polyethylene beads was 3000-6000 μm, wasfed into a 4″ diameter product container, which was a component of thefilter assembly shown in FIG. 1. Compressed air was fed into the inlethead until the pressure above the mixture was 10 psig for 15 minutes.The liquid, water, flowed through the filter assembly and into thedischarge head. The mixture in the product container after the filteringprocess had a water content of 3%.

[0058] The inlet head was depressurized and removed from the productcontainer. The detachable gas distribution plate was installed on theproduct container. The 4″ diameter product container was inverted so thegas distribution plate was on the bottom of the product container. Thedischarge head and detachable filter assembly were removed from theproduct container.

[0059] The product container and gas distribution plate were transportedto a fluid-bed dryer assembly shown in FIG. 4, where the upper plenumhad a larger diameter, 11″, than the product container, 4″. Thefluid-bed dryer assembly and product container were sealed, and a heatedair stream, 210° F., flowed up through the mixture of polyethylenebeads/water at such a rate, 330-360 ft/min at the distribution plate,whereby the bed behaved with slugging fluidization characteristics shownin FIG. 7. After the air stream fluidized the liquid/solid mixture for15 minutes, the water content of the mixture in the product bowl wasless than 0.01%.

[0060] Similar to Example 2, the filtration step in Example 3 removedthe majority of the liquid water, 47% of the aqueous solvent (liquidwater). However, the particle size of the plastic beads (3000-6000 μm)was much larger than the magnesium oxide (5-50 μm) or the titanium(250-420 μm).

[0061] The plastic beads, due to the size and shape of the beads,fluidized with slugging characteristics shown in FIG. 7. Therefore, theplastics beads were dried while behaving as a slugging fluidized bed.Although the solids in Examples 1, 2, and 3 fluidized differently, thefluid-bed apparatus was able to reduce the solvent content.

Example 4

[0062] A mixture of isopropyl alcohol, 75%, and polyethylene glycol,25%, where the particle range of the polyethylene glycol was 125-250 μm,was fed into a product container with a 4″ diameter at the gasdistribution assembly and a 11″ diameter at the filter assembly, whichwas a component of the filter assembly shown in FIG. 5. The height ofthe product container was 13″.

[0063] Nitrogen was fed into the inlet head until the pressure above themixture was 8 psig for 15 minutes. The liquid, isopropyl alcohol, flowedthrough the filter assembly and into the discharge head. The mixture inthe product container after the filtering process had an isopropylalcohol content of 30%.

[0064] The inlet head was depressurized and removed from the productcontainer. The detachable gas distribution plate was installed on theproduct container. The 4″ diameter product container was inverted so thegas distribution plate was on the bottom of the product container. Thedischarge head and detachable filter assembly were removed from theproduct container.

[0065] The product container and gas distribution plate were transportedto a fluid-bed dryer assembly shown in FIG. 4, where the upper plenumhad a larger diameter, 11″, than the distribution plate, 4″. Thefluid-bed dryer assembly and product container were sealed, and a heatednitrogen gas stream, 95° F., flowed up through the mixture ofpolyethylene glycol/Isopropyl alcohol at such a rate, 130-230 ft/min atthe distribution plate, whereby the bed behaved with smooth/bubblingfluidization characteristics shown in FIG. 7. After the nitrogen gasstream fluidized the liquid/solid mixture for 30 minutes, the isopropylalcohol content of the mixture in the product bowl was 100 ppm.

[0066] Example 4 shows a nitrogen gas stream used during the fluid-beddrying step. Nitrogen and other inert gases are commonly used to dry nonaqueous solvents to lower the oxygen concentration in the apparatus,which reduces the risk of an explosion.

[0067] During the fluid-bed drying step, the fluidizationcharacteristics went from bubbling to smooth, shown in FIG. 7, as thematerial was dried.

[0068] A different product container assembly, shown in FIG. 5, was usedin Example 4. The larger diameter of the filter assembly increases thesurface area of the filter cloth during the filtration step andincreases the expansion zone above the fluidized bed.

Example 5

[0069] A mixture of isopropyl alcohol, 85%, and polyethylene glycol,15%, where the particle range of the polyethylene glycol was 50-300 μm,was fed into a product container with a 16″ diameter at the gasdistribution assembly and a 16″ diameter at the filter assembly, whichwas a component of the filter assembly shown in FIG. 1. The height ofthe product container was 25″.

[0070] Argon was fed into the inlet head until the pressure above themixture was 60 psig for 60 minutes. The liquid, isopropyl alcohol,flowed through the filter assembly and into the discharge head. Themixture in the product container, a wet cake, after the filteringprocess had an isopropyl alcohol content of 45%.

[0071] The inlet head was depressurized and removed from the productcontainer. The detachable gas distribution plate was installed on theproduct container. The 16″ diameter product container was inverted sothe gas distribution plate was on the bottom of the product container.The discharge head and detachable filter assembly were removed from theproduct container.

[0072] The product container and gas distribution plate were transportedto a fluid-bed dryer assembly shown in FIG. 6, where the upper plenumhad a diameter, 16″, identical to the distribution plate, 16″. Thefluid-bed dryer assembly and product container were sealed, and a heatedargon gas stream, 95° F., flowed up through the mixture of polyethyleneglycol/isopropyl alcohol at such a rate, 100-240 ft/min at thedistribution plate, where the bed behaved with bubbling fluidizationcharacteristics shown in FIG. 7. After the argon gas stream fluidizedthe liquid/solid mixture for 120 minutes, the isopropyl alcohol contentof the mixture in the product bowl was 100 ppm.

[0073] Example 5 shows a larger product container, 16″ diameter, thanprevious examples, 4″ diameter. A different fluid-bed assembly, shown inFIG. 6, was also used for Example 5. Although more material was presentin above the fluidized bed of material in Example 5 than Example 4, thefluid-bed drying step adequately dried the material to moisture contentof 100 ppm.

[0074] The argon gas stream in Example 5 was recirculated. The gasstream from the fluid-bed dryer was passed through a condenser, whichremoved the majority of the solvent in the argon gas stream. The argongas stream was heated by a heat exchanger before being recirculated tothe fluid-bed dryer apparatus. Since a small amount of solvent wasrecirculated to the inlet of the fluid-bed dryer, the recyclingfluid-bed drying step took more time than the once through drying stepdescribed in Example 4.

Example 6

[0075] A mixture of isopropyl alcohol, 75%, and polyethylene glycol,25%, where the particle range of the polyethylene glycol was 100-500 μm,was fed into a product container with a 16″ diameter at the gasdistribution assembly and a 16″ diameter at the filter assembly, whichwas a component of the filter assembly shown in FIG. 1. The height ofthe product container was 25″.

[0076] Argon was fed into the inlet head until the pressure above themixture was 25 psig for 60 minutes. The liquid, isopropyl alcohol,flowed through the filter assembly and into the discharge head. Themixture in the product container, a dry cake, after the filteringprocess had an isopropyl alcohol content of 35%.

[0077] The inlet head was depressurized and removed from the productcontainer. The detachable gas distribution plate was installed on theproduct container. The 16″ diameter product container was inverted sothe gas distribution plate was on the bottom of the product container.The discharge head and detachable filter assembly were removed from theproduct container.

[0078] The product container and gas distribution plate were transportedto a fluid-bed dryer assembly shown in FIG. 6, where the upper plenumhad a diameter, 16″, identical to the distribution plate, 16″. Thefluid-bed dryer assembly and product container were sealed, and a heatedargon gas stream, 95° F., flowed up through the mixture of polyethyleneglycol/isopropyl alcohol at such a rate, 100-240 ft/min at thedistribution plate, whereby the bed behaved with bubbling fluidizationcharacteristics shown in FIG. 7. After the argon gas stream fluidizedthe liquid/solid mixture for 120 minutes, the isopropyl alcohol contentof the mixture in the product bowl was 100 ppm.

[0079] The average particle size of the polyethylene glycol described inExample 6 was larger than the average particle size described in Example5. Therefore, the argon gas stream flow rate was higher in Example 6,140-300 ft/min, than in Example 5, 100-240 ft/min, during the fluid-beddrying step. The higher gas flow rates were required because largerparticles, with the same particle density and shape, require higher gasvelocities for fluidization.

[0080] Example Parameters and Results

[0081] The filter/dryer procedure was performed for several mixtures ofbulk solids and liquids. The bulk solids ranged in size from 5 μm to 6mm in diameter. The liquids were aqueous and non aqueous. The results ofthe tests are shown in Table 1.

[0082] Selected Conclusions from Examples

[0083] 1) The filter/dryer assembly can remove liquids from bulk solidswith a wide range of particle size, 5 μm to 6 mm.

[0084] 2) The filter/dryer assembly also has the ability to removeaqueous and non-aqueous liquids from bulk solids.

[0085] 3) The initial moisture of the liquid/bulk solids feed to thefilter/dryer can be as high as 83% and yet still achieve good moistureremoval. TABLE I Diameter of Particle Operating Pressure EXAMPLEcontainer Range Initial of filter Moisture After No. Solid Liquid (in)(μm) Moisture (psig) Filtering 1 Magnisum Methyl 4  5-50 83% 20 31%Oxide Alcohol 2 Titanium Acetone 4 250-420 50% 10  2% Beads 3 PlasticWater 4 3000- 50% 10  3% Beads 6000 4 Polyethylene Isopropyl 4 125-25075% 8 30% Glycol Alcohol 5 Polyethylene Isopropyl 16  50-300 85% 60 45%Glycol Alcohol 6 Polyethylene Isopropyl 16 100-500 75% 25 35% GlycolAlcohol Fluidization Drying EXAMPLE Gas for Inlet gas Velocity TimeMoisture After No. Drying temperature (ft/min) (min) Fluid-BedObservations 1 Air 73 120-140 15 1.40% stiff cake after filtration cycle2 Air 70 280-320 15 0.01% free flowing 3 Air 210 330-360 15 0.00% freeflowing 4 Nitrogen 95 130-230 30 100 ppm began as a slurry and became afree flowing bulk solid 5 Argon 95 100-240 120 100 ppm requiredmechanical agitation during drying 6 Argon 95 140-300 120 100 ppm freeflowing

what is claimed is:
 1. A filter-dryer apparatus employing a singlecontainer for both filtering and drying operations, comprising: acontainer holding a material to be filtered and dried, adapted toconnect to a filter system and to connect to a fluid bed dryer system.2. The apparatus accordingly to claim 1, wherein the container includesa vessel having means for supporting said filter system.
 3. Theapparatus according to claim 2 wherein the vessel is cylindrical inshape.
 4. The apparatus according to claim 2 wherein the support meansincludes a detachable bottom plate.
 5. The apparatus according to claim2 wherein the filter system includes a filter sheet and a filter nettingbed, both anchored to the support means.
 6. The apparatus according toclaim 2, wherein the filter system is a pressurized filter system andthe container includes a gas distribution plate and a means forsupporting the gas distribution plate.
 7. The apparatus according toclaim 6, wherein the gas distribution plate support means includes adetachable upper plate.
 8. The apparatus according to claim 6, whereinthe gas distribution plate comprises at least one of a perforated,sintered, or grid plate.
 9. The apparatus according to claim 6, whereinthe gas distribution plate includes a retention screen.
 10. Theapparatus according to claim 6, wherein after completion of saidfiltration operation, a filtrate results and the container uponinversion includes the gas distribution plate supporting the filtrate.11. The apparatus accordingly to claim 1, wherein the container includesa vessel having means for connecting to said fluid bed dryer system. 12.The apparatus accordingly to claim 11, wherein the fluid-bed dryersystem consists of a lower plenum, an upper plenum, a dust collector,and a gas handling system.
 13. The apparatus accordingly to claim 12,wherein the gas handling system comprises at least one of a heater, apressure blower, and a condenser.
 14. The apparatus accordingly to claim12, wherein a filtering device in the upper plenum, removes particulatesin the gas stream.
 15. The apparatus accordingly to claim 12, furtherincluding means for recycling gas from said gas handling system to saidheater for reuse.
 16. A filter-dryer apparatus employing a singlecontainer for both filtering and drying operations, comprising: acontainer holding a material to be filtered and dried, adapted toconnect to a pressurized filter system and to connect to a fluid beddryer system.
 17. A process for separating particulates from liquids bythe operations of filtration and drying, which comprises the followingsteps: providing a single container for both filtering and dryingoperations; introducing a mixture of particles and liquid to saidcontainer; connecting the container to a filter system and filtering theparticulates from the liquid; detaching the container from the filtersystem; connecting the container to a fluid bed drying system andremoving the liquid from the particulates to result in dry particulates.18. The process of claim 17, wherein the liquid is selected from thegroup consisting of water, isopropyl alcohol, acetone, methyl alcohol,ethylene dichloride, methyl chloride, toluene, xylene, benzene, methylethyl ketone and hexane.
 19. The process of claim 17, wherein the liquidcontent of the particulate mixture is 15% -90%.
 20. The process of claim17, wherein the particulates have sphericity shape factors of 0.3 to1.0.
 21. The process of claim 17, wherein the particulate sizes rangefrom 1 μ to 20,000 μm.
 22. The process of claim 17, further includingthe step of inverting the container prior to connecting it to the fluidbed drying system.
 23. The process of claim 17, wherein the fluid beddrying system employs a gas stream adjusted so that the fluidizedparticulates behave in a regime selected from the group consisting offixed bed, incipient fluidization, smooth fluidization, bubblingfluidization, slugging fluidization.